CN109607652A - A kind of fluidized crystallization device and its technique - Google Patents
A kind of fluidized crystallization device and its technique Download PDFInfo
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- CN109607652A CN109607652A CN201811049501.3A CN201811049501A CN109607652A CN 109607652 A CN109607652 A CN 109607652A CN 201811049501 A CN201811049501 A CN 201811049501A CN 109607652 A CN109607652 A CN 109607652A
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- 238000002425 crystallisation Methods 0.000 title claims abstract description 75
- 230000008025 crystallization Effects 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000007789 gas Substances 0.000 claims abstract description 115
- 150000003839 salts Chemical class 0.000 claims abstract description 102
- 239000002351 wastewater Substances 0.000 claims abstract description 63
- 238000000889 atomisation Methods 0.000 claims abstract description 27
- 230000008569 process Effects 0.000 claims abstract description 21
- 230000006835 compression Effects 0.000 claims abstract description 3
- 238000007906 compression Methods 0.000 claims abstract description 3
- 235000002639 sodium chloride Nutrition 0.000 claims description 107
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- 239000003546 flue gas Substances 0.000 claims description 15
- JEGUKCSWCFPDGT-UHFFFAOYSA-N h2o hydrate Chemical group O.O JEGUKCSWCFPDGT-UHFFFAOYSA-N 0.000 claims description 14
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 13
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 12
- 238000006477 desulfuration reaction Methods 0.000 claims description 12
- 230000023556 desulfurization Effects 0.000 claims description 12
- 230000000694 effects Effects 0.000 claims description 11
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 9
- 239000011780 sodium chloride Substances 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 6
- 235000011152 sodium sulphate Nutrition 0.000 claims description 6
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 4
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 4
- 238000002309 gasification Methods 0.000 claims description 4
- 239000011734 sodium Substances 0.000 claims description 4
- 229910052708 sodium Inorganic materials 0.000 claims description 4
- 238000004523 catalytic cracking Methods 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 235000011132 calcium sulphate Nutrition 0.000 claims description 2
- 230000003009 desulfurizing effect Effects 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims description 2
- 235000019341 magnesium sulphate Nutrition 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 5
- 230000008676 import Effects 0.000 abstract description 4
- 238000009834 vaporization Methods 0.000 abstract description 3
- 230000008016 vaporization Effects 0.000 abstract description 3
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 238000003912 environmental pollution Methods 0.000 abstract 1
- 239000003517 fume Substances 0.000 abstract 1
- 230000000052 comparative effect Effects 0.000 description 6
- 230000008859 change Effects 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- AFCARXCZXQIEQB-UHFFFAOYSA-N N-[3-oxo-3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propyl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(CCNC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 AFCARXCZXQIEQB-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000005713 exacerbation Effects 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000002667 nucleating agent Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002352 surface water Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/10—Treatment of water, waste water, or sewage by heating by distillation or evaporation by direct contact with a particulate solid or with a fluid, as a heat transfer medium
- C02F1/12—Spray evaporation
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Treating Waste Gases (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
Heat source progress fluidized crystallization device and its technique are done using fume afterheat or compression cyclic steam the present invention relates to a kind of, including crystallisation vessel and air-flow ingress pipe, by that will have the gas of certain nuclei of crystallization salt particle to import in crystallization apparatus by air-flow ingress pipe, and it is directly sprayed onto after being atomized high slat-containing wastewater by atomising device on nuclei of crystallization salt particle, the contact of gas containing salt grain that the atomization waste water being adsorbed in salt grain imports in uphill process and through air-flow ingress pipe, heat vaporization is absorbed in the higher saliferous gas of the atomization waste water temperature being adsorbed in salt grain, salt direct crystallization is on the nuclei of crystallization；To thoroughly realize the complete removing of salt in high slat-containing wastewater, allow to meet direct emission, purpose free from environmental pollution.
Description
Technical field
The present invention relates to a kind of fluidized crystallization device and its techniques, belong to environmental technology field.
Background technique
As country is to the further requirement of environmental protection, in order to execute national emission standard, many enterprise constructions steam power plant
Flue gas desulfurization, catalytic cracking flue gas desulfurization generate the very high sewage of salt content.It is produced simultaneously when producing demineralized water a large amount of
High slat-containing wastewater.In addition, there is many production environments to need to carry out circulating water, such as large scale industry Air-conditioning Cycle in industry
Water is cooling, in order to prevent equipment corrosion and fouling, and recirculated water needs are periodically discharged, and by the recirculated water using discharge
So become high slat-containing wastewater.Certainly, in industrial environment, high slat-containing wastewater, such as water process can be generated there are also many situations
The high slat-containing wastewater etc. generated in the high slat-containing wastewater and coal chemical industry production process generated in the process.
High slat-containing wastewater contains a large amount of dissolubility salt, can be tight if direct emission will finally enter surface water system
Ghost image Xiangshui County weight in turn results in and the salt content of water body is received to increase significantly, exacerbation dead so as to cause limnobios population
Saline Land problem.If being directly discharged into domestic sewerage systems to be handled, and it be easy to cause micro- in processing system biochemistry pool
Biological mortality, effluent quality deteriorate, and especially for the sewage treatment plant for having Treated sewage reusing function, will result directly in reuse
Middle water water quality reduce.As it can be seen that high slat-containing wastewater outlet has great destruction to environment.Height increasingly by country
Degree is paid attention to.
Currently, the high slat-containing wastewater zero-discharge technology of research economy is important technological difficulties.In the prior art, commonly
Falling film evaporation is usually used in high slat-containing wastewater treatment process or multiple-effect evaporation is handled, but above-mentioned means cost compared with
Height, investment is high, easy fouling, difficult long-period stable operation.
Summary of the invention
The present invention provides a kind of new fluidized crystallization devices and corresponding technique, for handling high slat-containing wastewater.
In order to solve the above technical problems, the present invention is achieved by the following technical solutions:
A kind of fluidized crystallization device comprising:
There is waterwater entrance, salt mouth and gas access is added, be provided with atomizer at waterwater entrance for crystallisation vessel (2)
(4), gas access is connected with gas introduction tube (12)；
Salt is dry settler (5), has shell, upper part of the housing is provided with gas vent (10)；Salt is provided on shell to go out
Mouth (9)；
The bottom end of the top perforation salt dry settler (5) of crystallisation vessel (2) enters in container, in crystallisation vessel (2)
Top is connected with the first cyclone separator (7)；
The waterwater entrance and gas access, which are arranged, dries settler (5) outside in the salt.
It is preferred that being connected with the second cyclone separator (8) with gas vent in shell.
Second cyclone separator (8) is provided with second level cyclonic separation.
Salt outlet be it is multiple, be additionally provided with salt nuclei of crystallization circulation pipe (6), described salt nuclei of crystallization circulation pipe (6) one end
It exports and connects with any salt, the other end is connected to gas introduction tube (12).
It is preferred that waterwater entrance is connected with wastewater heat exchange device (3), or followed in gas introduction tube (12) far from the salt nuclei of crystallization
One end of endless tube (6) is connected with first gas heat exchanger (111), or is connected with second gas heat exchange with gas vent
Device (11).
It is preferred that being connected with gas compressor (1) with first gas heat exchanger (111).
It is preferred that the atomizer (4) be provided with it is multiple, and centered on axial direction be symmetrical arranged.
The present invention further discloses a kind of fluidized crystallization method comprising following steps:
The gas of saliferous and waste water through being atomized, the liquid gasification in waste water is gas, saline crystallization discharge；
The temperature of the gas of saliferous is 70-300 DEG C.
It is preferred that waste water carries out atomization process to waste water through atomizer；Salt is under gas effect in suspended state and mist
Change waste water；The temperature of the gas of saliferous is 70-300 DEG C.
It is preferred that being recycled after gas or saline crystallization after heat exchange, saliferous gas is formed；
Waste water carries out atomization process again after heat exchange；
Gas after gasification exchanges heat after compression；
The temperature of the gas of saliferous is 140-180 DEG C.
The partial size of salt is 30um-3mm, preferably 60-300um in the saliferous gas.
The gas is the gases such as high-temperature flue gas, flue gas, hot-air or hot nitrogen；The waste water is FCC desulfurization wastewater, pot
It is drained outside kiln gas desulphurization denitration waste water, catalytic cracking and desulfurizing denitration wastewater, desalting water treatment station concentrated water, recirculated water；The salt
For one of sodium chloride, sodium sulphate, calcium sulfate, magnesium sulfate, vulcanized sodium or a variety of；The additional amount of salt is the 5%- of material position volume
15%.
The above technical solution of the present invention has the following advantages over the prior art:
Fluidized crystallization device of the present invention, including crystallisation vessel and the dry settler of salt, by that will have certain salt
The gas of particle imports crystallisation vessel, and high slat-containing wastewater is carried out atomization process to atomized useless by atomising device
Water, atomization waste water are sprayed directly on on the salt nuclei of crystallization, and water absorbs heat vaporization in flue gas, and the salt in waste water is directly in the salt nuclei of crystallization
Upper crystallization has effectively achieved the purified treatment to waste water, and can prevent from crystallizing on the reactor wall, it is ensured that device long week
Phase stable operation.
From the point of view of technological angle, in reaction, heat source and fluidizing gas is done using flue gas, does not need that heat source is provided separately,
Operating cost is very low.In addition, the salt grain generated in crystallization process can also directly cook the salt nuclei of crystallization, it is recycled, is not required to outer
Added Nucleating Agents, it is at low cost.
Fluidized crystallization reaction process is made of salt crystallization reaction and salt drying program, and when reaction, salt does not need to set up setting
It is dried in drying system, and process flow is short, small investment.
Detailed description of the invention
In order to make the content of the present invention more clearly understood, it below according to specific embodiments of the present invention and combines
Attached drawing, the present invention is described in further detail, wherein
Fig. 1 is the structural schematic diagram of fluidized crystallization device of the present invention；
Fig. 2 is another structural schematic diagram of fluidized crystallization device of the present invention；
Appended drawing reference indicates in figure are as follows: 1- gas compressor, 2- crystallisation vessel, 3- wastewater heat exchange device, 4- atomizer, 5-
Salt dries settler, 6- salt nuclei of crystallization circulation pipe, the first cyclone separator of 7-, the second cyclone separator of 8-, the outlet of 9- salt, 10-
Gas vent, 111- first gas heat exchanger, 11- second gas heat exchanger, 12- gas introduction tube.
Specific embodiment
In order to better understand the content of the present invention, below with reference to the mode of specific implementation the present invention is explained and
Explanation.
Embodiment 1: device
Present embodiment discloses a kind of fluidized crystallization devices comprising crystallisation vessel 2 and the dry settler 5 of salt, in which:
It is provided with waterwater entrance, salt addition mouth and gas access in crystallisation vessel 2, is provided at waterwater entrance for inciting somebody to action
Waste water carries out the atomizer 4 of atomization process, and gas access is connected with gas introduction tube 12；Wherein, for waterwater entrance
With the setting of atomizer 4, generally all it is alternatively provided in crystallisation vessel 2 and close bottom end can be each from the point of view of quantity is arranged
It is multiple from being all respectively set, and when atomizer 4 is arranged multiple, preferably with crystallisation vessel 2 it is axial be that symmetry axis is symmetrically set two-by-two
It sets.
The structure of settler 5 dry for salt, with shell, upper part of the housing is provided with gas vent 10；It is set on shell
It is equipped with salt outlet 9；The salt outlet can be set to one, may be set to be multiple, it is preferable that be additionally provided with the salt nuclei of crystallization and follow
Endless tube 6, one end and the outlet of any salt connect, and the other end is connected to gas introduction tube 12.
The bottom end of the dry settler 5 of top perforation salt of crystallisation vessel 2 enters in container, connects on the top of crystallisation vessel 2
It connects and is provided with the first cyclone separator 7；The purpose of the separator is carried out to the gas containing salt crystallization after fluidization treatment
Preliminary cyclonic separation obtains gas and salt crystallization.When setting, waterwater entrance and gas access are arranged at the dry settler of salt
Outside 5.
On the basis of the above embodiments, in order to be better achieved fluidisation after saliferous crystallize gas separation, so
It is connected with the second cyclone separator 8 with gas vent in shell, fine point can be then further realized using the separator
From.It is preferred that second cyclone separator 8 is second level cyclonic separation, naturally it is also possible to need to select to be set as multistage according to industry.
As can be with further preferred embodiment, in order to realize making full use of for energy, in the base of above-described embodiment
On plinth, preferably waterwater entrance is connected with wastewater heat exchange device 3, or in gas introduction tube 12 far from salt nuclei of crystallization circulation pipe 6
One end is connected with gas heat exchanger 111, or is connected with second gas heat exchanger 11 with gas vent, so as to right
Waste water, gas with certain temperature carry out further heat exchange processing.
Furthermore it is preferred that being connected with gas compressor 1 with first gas heat exchanger 111.
When in use, the course of work is as follows for above-mentioned apparatus: firstly, when driving for the first time mouth being added through salt, knot being added in salt
In brilliant container, after device is stablized, the salt grain as the salt nuclei of crystallization flow to gas along salt nuclei of crystallization circulation pipe 6 from top to bottom and imports
In pipe 12, gas enters through gas introduction tube at the same time, mixes with the salt grain flowing in gas introduction tube, in order to guarantee to mix
Effect is closed, the gas for preferably comprising flue gas or steam enters through gas compressor pressurization, and the salt nuclei of crystallization are brushed to form stream by gas
Change state and gas enters in crystallisation vessel together, flows from bottom to top；Hold at this point, waste water also enters crystallization after atomization process
In device, the waste water after atomization and the gas contact with certain temperature, the crystalline particle in flow process, after atomization in waste water
Encountering gas realizes vaporization, while the crystalline particle in waste water contacts in flowing the salt nuclei of crystallization in gas and is adsorbed,
And rise with gas；Later, into the first cyclone separator carry out crude separation, in order to improve separating effect, preferably further into
Enter the second cyclone separator further to be separated, gas and salt grain are separated, gas is through gas vent delivery line, and salt grain is then
The natural subsidence in the dry settler of salt, during decline, with the high-temperature gas flowed from bottom to top in the dry settler of salt
Mass-and heat-transfer occurs for counter current contacting, and remaining waste water moisture content is thoroughly dried in salt grain.Later, the salt after sedimentation can recycle
It uses.
Embodiment 2
Present embodiment discloses a kind of fluidized crystallization methods, include the following steps:
Atomization process is carried out to FCC desulfurization wastewater；
The salt that partial size is 60um is added in the hot-air of flow regime, to form the gas of saliferous, salt is in gas
Salt grain exchange is carried out with atomization waste water in suspended state under effect；
The temperature of the gas of saliferous is 70-300 DEG C.
Wherein, salt is the mixture of sodium chloride and sodium sulphate, and the volume ratio of sodium chloride and sodium sulphate is 1: 3 in mixture,
5% that total amount is material position volume is added.
Embodiment 3
Present embodiment discloses a kind of fluidized crystallization methods, include the following steps:
Atomization process is carried out to FCC desulfurization wastewater；
The salt that partial size is 300um is added in the hot nitrogen of flow regime, to form the gas of saliferous, salt is in gas
Salt grain exchange is carried out with atomization waste water in suspended state under effect；
The temperature of the gas of saliferous is 70-300 DEG C.
Wherein, salt is sodium sulphate, and additional amount is the 8% of material position volume.
Embodiment 4
Present embodiment discloses a kind of fluidized crystallization methods, include the following steps:
Atomization process is carried out to FCC desulfurization wastewater；
The salt that partial size is 30um is added in the high-temperature flue gas of flow regime, to form the gas of saliferous, salt is in gas
Salt grain exchange is carried out with atomization waste water in suspended state under body effect；
The temperature of the gas of saliferous is 300 DEG C.
Wherein, salt is calcium sulfate, and additional amount is the 10% of material position volume.
Embodiment 5
Present embodiment discloses a kind of fluidized crystallization methods, include the following steps:
Atomization process is carried out to FCC desulfurization wastewater；
The salt that partial size is 1mm is added in the high-temperature flue gas of flow regime, to form the gas of saliferous, salt is in gas
Salt grain exchange is carried out with atomization waste water in suspended state under effect；
The temperature of the gas of saliferous is 140 DEG C.
Wherein, salt is vulcanized sodium, and additional amount is the 15% of material position volume.
Embodiment 6
Present embodiment discloses a kind of fluidized crystallization methods, include the following steps:
Atomization process is carried out by draining outside recirculated water；
The salt that partial size is 3mm is added in the high-temperature flue gas of flow regime, to form the gas of saliferous, salt is in gas
Salt grain exchange is carried out with atomization waste water in suspended state under effect；
The temperature of the gas of saliferous is 180 DEG C.
Wherein, salt is vulcanized sodium, and additional amount is the 15% of material position volume.
Comparative example 1
This comparative example discloses a kind of fluidized crystallization method, includes the following steps:
Atomization process is carried out to FCC desulfurization wastewater；
The salt that partial size is 20um is added in the high-temperature flue gas of flow regime, to form the gas of saliferous, salt is in gas
Salt grain exchange is carried out with atomization waste water in suspended state under body effect；
The temperature of the gas of saliferous is 180 DEG C.
Wherein, salt is calcium sulfate, and additional amount is the 10% of material position volume.
Comparative example 2
This comparative example discloses a kind of fluidized crystallization method, includes the following steps:
Atomization process is carried out to FCC desulfurization wastewater；
The salt that partial size is 30um is added in the high-temperature flue gas of flow regime, to form the gas of saliferous, salt is in gas
Salt grain exchange is carried out with atomization waste water in suspended state under body effect；
The temperature of the gas of saliferous is 160 DEG C.
Wherein, salt is calcium sulfate, and additional amount is the 10% of material position volume.
In above-described embodiment and comparative example, used high slat-containing wastewater is FCC desulfurization wastewater, wherein test data
It has been shown that, sodium sulphate content 4-5%, solid content 7-8%, COD 50-60.It is drained outside used recirculated water, through surveying
Examination, data show that TDS content is 0.4%, solid content 50-120mg/m3, COD 50-80.
After above-described embodiment 2-6 and comparative example 1-2 processing, data are as follows:
It is elaborated although the present invention has passed through above-mentioned specific embodiment, the common skill of this profession
Art personnel should be understood that made on this basis without departing from any form of claims and the change of details
Change, belongs to invention which is intended to be protected.
Claims (12)
1. a kind of fluidized crystallization device characterized by comprising
There is waterwater entrance, salt mouth and gas access is added, be provided with atomizer (4) at waterwater entrance for crystallisation vessel (2),
Gas access is connected with gas introduction tube (12)；
Salt is dry settler (5), has shell, upper part of the housing is provided with gas vent (10)；Salt outlet is provided on shell
(9)；
The bottom end of the top perforation salt dry settler (5) of crystallisation vessel (2) enters in container, on the top of crystallisation vessel (2)
It is connected with the first cyclone separator (7)；
The waterwater entrance and gas access, which are arranged, dries settler (5) outside in the salt.
2. fluidized crystallization device according to claim 1, which is characterized in that be connected in shell with gas vent
Second cyclone separator (8).
3. fluidized crystallization device according to claim 2, which is characterized in that second cyclone separator (8) is provided with
Second level cyclonic separation.
4. fluidized crystallization device according to claim 1 to 3, which is characterized in that salt outlet be it is multiple, also set
It is equipped with salt nuclei of crystallization circulation pipe (6), the salt nuclei of crystallization circulation pipe (6) one end and the outlet of any salt connect, the other end and gas
Ingress pipe (12) connection.
5. fluidized crystallization device according to claim 4, which is characterized in that waterwater entrance is connected with wastewater heat exchange device
(3), or in gas introduction tube (12) first gas heat exchanger is connected with far from one end of salt nuclei of crystallization circulation pipe (6)
(111), second gas heat exchanger (11) or with gas vent are connected with.
6. fluidized crystallization device according to claim 5, which is characterized in that connect and set with first gas heat exchanger (111)
It is equipped with gas compressor (1).
7. -6 any fluidized crystallization device according to claim 1, which is characterized in that the atomizer (4) is provided with
It is multiple, and be symmetrical arranged centered on axial direction.
8. a kind of fluidized crystallization method, includes the following steps:
The gas of saliferous and waste water through being atomized, the liquid gasification in waste water is gas, saline crystallization discharge；
The temperature of the gas of saliferous is 70-300 DEG C.
9. according to the method described in claim 8, it is characterized in that, waste water carries out atomization process to waste water through atomizer；Salt
Gas effect under in suspended state and atomization waste water；The temperature of the gas of saliferous is 70-300 DEG C.
10. method according to claim 8 or claim 9, which is characterized in that after the gas or saline crystallization after heat exchange, circulation
It uses, forms saliferous gas；
Waste water carries out atomization process again after heat exchange；
Gas after gasification exchanges heat after compression；
The temperature of the gas of saliferous is 70-300 DEG C.
11. method according to claim 8 or claim 9, which is characterized in that the partial size of salt is 30um- in the saliferous gas
3mm, preferably 60-300um.
12. according to the method for claim 11, which is characterized in that the gas is high-temperature flue gas, flue gas, hot-air or heat
The gases such as nitrogen；The waste water is FCC desulfurization wastewater, boiler flue gas desulfurization denitration wastewater, catalytic cracking and desulfurizing denitration wastewater, removes
It is drained outside saline treatment station concentrated water, recirculated water；The salt is sodium chloride, sodium sulphate, calcium sulfate, magnesium sulfate, one in vulcanized sodium
Kind is a variety of；The additional amount of salt is the 5%-15% of material position volume.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201811049501.3A CN109607652A (en) | 2018-09-10 | 2018-09-10 | A kind of fluidized crystallization device and its technique |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811049501.3A CN109607652A (en) | 2018-09-10 | 2018-09-10 | A kind of fluidized crystallization device and its technique |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113666391A (en) * | 2021-09-01 | 2021-11-19 | 西安交通大学 | Device for strengthening salt spray dehydration by using high-temperature salt particles and working method |
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| JP2010046607A (en) * | 2008-08-22 | 2010-03-04 | Kurita Water Ind Ltd | Crystallizer |
| CN103344093A (en) * | 2013-06-09 | 2013-10-09 | 山东奥诺能源科技有限公司 | Vertical type continuous fluidized bed pelleting drying device and method |
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| CN113666391A (en) * | 2021-09-01 | 2021-11-19 | 西安交通大学 | Device for strengthening salt spray dehydration by using high-temperature salt particles and working method |
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